System and method for softening water for use in a scrubber

ABSTRACT

The present invention relates generally to the field of emission control equipment for boilers, heaters, kilns, or other flue gas-, or combustion gas-, generating devices (e.g., those located at power plants, processing plants) and, in particular to a new and useful method and apparatus designed to improve the water supplied to non-calcium-based, aqueous wet SO x  scrubbers. In another embodiment, the present invention relates to a system and method for softening water for use in non-calcium-based, aqueous wet SO x  scrubbers.

FIELD AND BACKGROUND OF THE INVENTION

1. Field of the Invention

The present invention relates generally to the field of emission controlequipment for boilers, heaters, kilns, or other flue gas-, or combustiongas-, generating devices (e.g., those located at power plants,processing plants) and, in particular to a new and useful method andapparatus designed to improve the water supplied to non-calcium-based,aqueous wet SO_(x) scrubbers. In another embodiment, the presentinvention relates to a system and method for softening water for use innon-calcium-based, aqueous wet SO_(x) scrubbers.

2. Description of the Related Art

Sulfur appears in the life cycle of most plants and animals. Most sulfuremitted to the atmosphere originates in the form of hydrogen sulfidefrom the decay of organic matter. These emissions slowly oxidize tosulfur dioxide (SO₂). Under atmospheric conditions, SO₂ is a reactive,acrid gas that can be rapidly assimilated back to the environment.However, the combustion of fossil fuels, in which large quantities ofSO₂ are emitted to relatively small portions of the atmosphere, canstress the ecosystem in the path of these emissions. As used herein, SO₂and SO₃ emissions may generally be referred to as sulfur oxides orSO_(x) emissions.

Man is responsible for the majority of the SO₂ emitted to theatmosphere. Annual worldwide emissions are generally accepted to be over160 million tons, nearly half of which are from industrial sources. Thetwo principal industrial sources are fossil fuel combustion andmetallurgical ore refining.

When gaseous SO₂ combines with liquid (I) water, it forms a diluteaqueous solution of sulfurous acid (H₂SO₃). Sulfurous acid can easilyoxidize in the atmosphere to form sulfuric acid (H₂SO₄). Dilute sulfuricacid is a major constituent of acid rain. Nitric acid is the other majoracidic constituent of acid rain. The respective reactions are written asfollows:SO(g)+H₂O(l)→H₂SO₃(aq)  (1)O₂(g)+2H₂SO₃(aq)→2H₂SO₄(aq)  (2)

SO₂ can also oxidize in the atmosphere to produce gaseous sulfurtrioxide (SO₃). Sulfur trioxide reactions are written as follows:2SO₂(g)+O₂(g)→2SO₃(g)  (3)SO₃(g)+H₂O(g)→H₂SO₄(l)  (4)

While Equations 1 and 2 describe the mechanism by which SO₂ is convertedto sulfuric acid in acid rain, Equations 3 and 4 characterize drydeposition of acidified dust particles and aerosols.

The pH scale, a measure of the degree of acidity or alkalinity, is themethod used to quantify the acidity of acid rain.

Pure water has a pH of 7 and is defined as neutral, while lower valuesare defined as acidic and higher values as alkaline. If rainwatercontained no sulfuric or nitric acid, its pH would be approximately 5.7due to absorption of carbon dioxide (CO₂) from the atmosphere. Thecontributions of man-made SO₂ and nitrogen oxides (NO_(x)) furtherreduce the pH of rainwater. No uniformly accepted definition exists asto what pH constitutes acid rain. Some authorities believe that a pH ofabout 4.6 is sufficient to cause sustained damage to lakes and forestsin the northeastern portion of North America and in the Black Forestregion of Europe.

SO₂ Emissions Regulations:

Legislative action has been responsible for most industrial SO₂controls. Major landmark regulations include the Clean Air ActAmendments of 1970, 1977 and 1990 in the United States (U.S.), theStationary Emissions Standards of 1970 in Japan, and the 1983 SO₂Emissions Regulations of the Federal Republic of Germany. Since themid-1980s, SO₂ emissions regulations have been implemented in most otherindustrialized nations and many developing nations.

SO₂ Control:

Most utilities have adopted one of two strategies for SO₂ control,either switching to low sulfur coal or installing scrubbers. A varietyof SO₂ control processes and technologies are in use and others are invarious stages of development. Commercialized processes include wet,semidry (slurry spray with drying) and completely dry processes. The wetflue gas desulfurization (WFGD) scrubber is the dominant worldwidetechnology for the control of SO₂ from utility power plants, withapproximately 85% of the installed capacity, although the dry flue gasdesulfurization (DFGD) systems are also used for selected lower sulfurapplications.

Total annual SO₂ emissions in the U.S., including electric utility SO₂emissions, have declined since 1970 as various regulations have beenadopted. During the same period, electricity generation from coal hasalmost tripled (see Table 1 below).

TABLE 1 U.S. SO₂ Emissions and Coal-Fired Power Generation Total U.S.SO₂ Utility SO₂ Coal Fired Utility Year 10⁶ t/yr 10⁶ t/yr Generation10¹² kWh 1970 31 17 0.7 1980 26 17 1.2 1990 23 16 1.6 2000 16 11 2.0

A significant portion of this emissions reduction has been the result ofswitching to low sulfur coal, predominantly from the western U.S. In1970 virtually all of the utility coal came from the eastern, highersulfur coal fields, while by 2000 approximately half of the coal camefrom western low sulfur sources. Slightly less than two-thirds of SO₂emission reductions have been attributed to fuel switching while over athird has been through the installation of flue gas desulfurizationsystems, predominantly wet scrubbers. More than 50% of the U.S.coal-fired capacity already has FGD systems installed and operating.This may increase to more than 80% over the next decade and a half asexisting regulations are implemented and proposed regulations areadopted.

Wet Scrubbers—Reagents:

Wet scrubbing processes are often categorized by reagent and otherprocess parameters. The primary reagent used in wet scrubbers islimestone. However, any alkaline reagent can be used, especially wheresite-specific economics provide an advantage. Other common reagents arelime (CaO), magnesium enhanced lime (MgO and CaO), ammonia (NH₃), andsodium carbonate (Na₂CO₃). In the case of sodium carbonate (Na₂CO₃),scrubbers based on this chemistry suffer scaling problems due to thepresence of dissolved calcium in the makeup water. Scaling problemsrequire unit outages for cleaning WFGD absorbers every 6 to 8 months.This puts soda based scrubbers at a disadvantage compared to limestonebased WFGD.

The process by which soda, or sodium carbonate, wet scrubbers operate iswell known to those of skill in the art. For example, one suitablereaction process is detailed in Sulfur Oxides Control Technology Series:Flue Gas Desulfurization Dual Alkali Process (EPA Document 625/8-80-004,October 1980), the text of which is hereby incorporated by reference asthough fully set forth herein in its entirety.

In one instance, natural fresh water is used as the base stock for theraw makeup water. Such waters, prior to treatment, contain varyingamounts of inorganic impurities, the most common being dissolvedcalcium, magnesium, iron, carbonates, and sulfates in ionic form. Waterthat has not been treated to remove any of these impurities is sometimesreferred to as raw water. The total carbonate content in the raw wateris referred to informally as the total alkalinity. The hardness of thewater is in turn determined directly by the total amount of calcium andmagnesium. The term generally refers to the negative effect that theseions have on the ability of soaps and detergents to lather in hardwater. In the context of a wet scrubber that uses sodium hydroxide,sodium carbonate, or sodium bicarbonate as a reagent to scrub sulfurdioxide from a flue gas, or combustion gas, the concern about thehardness constituents in the raw water is that as raw water becomesexposed to the scrubber solutions inside the wet scrubber, the calciumions will react with carbonate ions, sulfite and bisulfite ions andsulfate ions to form solid calcium carbonate, solid calcium sulfite, andsolid calcium sulfate. Such solid compounds tend to deposit on theinternals of the scrubber causing scaling sufficient to render thescrubber inoperable. Such a situation requires, at some point, theoperator of the facility to shut such a “fouled” scrubber down longenough to enter the scrubber and manually clean it out. Such anoperation involves significant time in lost production and physicalcleaning expenses. To mitigate such detrimental consequences, anoperator attempts to reduce the amount of hardness in the raw water bytreating that water prior to use in such a scrubber. One suchconventional treatment method is depicted in FIG. 1.

As is illustrated in FIG. 1, conventional system 100 includes flocsupply line 102, sodium carbonate (Na₂CO₃) solution supply line 103, rawwater supply line 104 and lime supply 106. Lime supply 106 supplies limeto detention slaker 108. Detention slaker 108 includes therein at leastone agitating device (e.g., a mixer) and is provided with a water supplyline to permit the mixing of the lime from lime supply 106 with water toyield a lime slurry that is supplied, via lime slurry supply line 110,to precipitator/crystallizer 112. Also supplied toprecipitator/crystallizer 112 are floc via floc supply line 102, sodiumcarbonate solution via sodium carbonate supply line 103 and raw watervia raw water supply line 104. Precipitator/crystallizer 112 alsoincludes at least one agitating device (e.g., a mixer) to facilitate themixing of the sodium carbonate solution, floc, raw water and limeslurry. Once any undesirable solids are permitted to “settle out” and/orprecipitate to the bottom of precipitator/crystallizer 112, this treatedsolution of sodium carbonate solution, lime, raw water and floc issupplied via supply line 114 to a settler/thickener 116. Insettler/thickener 116 the once-treated mixture of sodium carbonatesolution, lime, raw water and floc is further treated to removeadditional unwanted solid particles via the use of one or more agitatingdevices (e.g., a mixer). The solids generated by this process are thensupplied, with an appropriate amount of solution, to a sludge pond 122,via supply line 118, to permit further settling and reclamation of thesolids contained in such a waste solution. Additionally, or in somecases optionally, a portion of the solids generated by settler/thickener116 are re-supplied, with an appropriate amount of solution, toprecipitator/crystallizer 112 via supply line 120 to supply seedcrystals for the precipitation stage.

Once any undesirable solids are permitted to “settle out” and/orprecipitate to the bottom of settle/thickener 116, the twice-treatedsolution of sodium carbonate solution, lime, raw water and floc issupplied via supply line 124 to treated water tank 126. In treated watertank 126 the twice treated solution of sodium carbonate solution, lime,raw water and floc is combined with sulfuric acid (H₂SO₄) from sulfuricacid tank 130 via sulfuric acid supply line 132. This combination oftwice-treated solution and sulfuric acid is then further agitated via asuitable device (e.g., a mixer) until a desired pH is obtained. Oncethis occurs, the suitably treated solution is supplied to a wet scrubbervia supply line 134.

As is known to those of skill in the art, lime softening works byraising the pH of the raw water and causing the bicarbonate to convertto carbonate and then precipitating the calcium as calcium carbonate.Once the pH rises to above about 10, magnesium starts to precipitate asmagnesium hydroxide. FIG. 2 is a plot of the calcium and magnesiumconcentration of a raw water that contains only calcium and magnesiumcarbonates and bicarbonates. Note that the calcium concentrationactually begins to rise as the magnesium drops above a pH of 10.

Given the data contained in FIG. 2, the only way that one could achieveboth low magnesium and low calcium values would be to perform thesoftening in two stages. First, one has to raise the pH to 11 and afterseparating out the precipitates, lower the pH back to 10 with, forexample, sulfuric acid to precipitate out the excess calcium as calciumcarbonate.

If raw water contains only calcium and magnesium sulfates, then limesoftening will remove no calcium at all but the magnesium will beremoved at a pH above 10. That is confirmed via the data shown in FIG.3. So lime softening does have the capacity to reduce calciumconcentration if the raw water contains principally calcium carbonate.But to remove both calcium and magnesium, the system must be operated intwo stages. Removing the magnesium at a pH above 11 and then reducingthe calcium at a pH around 10.

Given the above, a need exists for a method and/or apparatus thatprovides for an efficient manner by which to remove the undesirablecalcium ions from the raw water used for make-up in non-calcium-based,aqueous wet SO_(x) scrubbers.

SUMMARY OF THE INVENTION

The present invention relates generally to the field of emission controlequipment for boilers, heaters, kilns, or other flue gas-, or combustiongas-, generating devices (e.g., those located at power plants,processing plants) and, in particular to a new and useful method andapparatus designed to improve the water supplied to non-calcium-based,aqueous wet SO_(x) scrubbers. In another embodiment, the presentinvention relates to a system and method for softening water for use innon-calcium-based, aqueous wet SO_(x) scrubbers.

Accordingly, one aspect of the present invention is drawn to a systemdesigned to treat and/or soften raw water supplied to anon-calcium-based, aqueous wet SO_(x) scrubber, the system comprising:(a) at least one floc supply means; (b) at least one raw water supplymeans; (c) at least one sodium carbonate supply means; (d) at least onewaste liquor supply means, wherein the waste liquor is supplied from aportion of the waste liquor generated by at least one non-calcium-based,aqueous wet SO_(x) scrubber; (e) at least one precipitator/crystallizertank, wherein the at least one floc supply means, the at least one rawwater supply means, the at least one sodium carbonate supply means andthe at least one waste liquor supply means all supply their respectivecompounds to the at least one precipitator/crystallizer tank, andwherein the at least one precipitator/crystallizer tank has at least oneoutlet; and (f) at least one settler/thickener tank that is in fluidcommunication with the at least one outlet of the at least oneprecipitator/crystallizer tank, the at least one settler/thickener tankhaving at least one outlet designed to supply treated water to anon-calcium-based, aqueous wet SO_(x) scrubber.

Another aspect of the present invention is drawn to a system designed totreat and/or soften raw water supplied to a non-calcium-based, aqueouswet SO_(x) scrubber, the system comprising: (a) at least one floc supplymeans; (b) at least one raw water supply means; (c) at least one sodiumcarbonate supply means; (d) at least one lime slurry supply means; (e)at least one first precipitator/crystallizer tank, wherein the at leastone floc supply means, the at least one raw water supply means, the atleast one sodium carbonate supply means and the at least one lime slurrysupply means all supply their respective compounds to the at least onefirst precipitator/crystallizer tank, and wherein the at least one firstprecipitator/crystallizer tank has at least one outlet; (f) at least onefirst settler/thickener tank that is in fluid communication with the atleast one outlet of the at least one first precipitator/crystallizertank, the at least one first settler/thickener tank having at least oneoutlet; (g) at least one second precipitator/crystallizer tank that isin fluid communication with the at least one outlet of the at least onefirst settler/thickener tank, wherein the at least one secondprecipitator/crystallizer tank has at least one outlet; (h) at least onewaste liquor supply means, wherein the at least one waste liquor supplymeans is in fluid communication with the at least one secondprecipitator/crystallizer tank, wherein the waste liquor is suppliedfrom a portion of the waste liquor generated by at least onenon-calcium-based, aqueous wet SO_(x) scrubber, and wherein the at leastone waste liquor supply means supplies waste liquor to the at least onesecond precipitator/crystallizer tank to precipitate excess calcium; and(i) at least one second settler/thickener tank that is in fluidcommunication with the at least one outlet of the at least one secondprecipitator/crystallizer tank, the at least one secondsettler/thickener tank having at least one outlet designed to supplytreated water to a non-calcium-based, aqueous wet SO_(x) scrubber.

In one instance, the above systems utilize less than about 7% by volumeof the waste liquor produced by a non-calcium-based, aqueous wet SO_(x)scrubber to treat and/or soften raw water for a non-calcium-based,aqueous wet SO_(x) scrubber. In another instance, the above systemsutilize less than about 5% by volume of the waste liquor produced by anon-calcium-based, aqueous wet SO_(x) scrubber to treat and/or softenraw water for a non-calcium-based, aqueous wet SO_(x) scrubber. In stillanother instance, the above systems utilize less than about 3% by volumeof the waste liquor produced by a non-calcium-based, aqueous wet SO_(x)scrubber to treat and/or soften raw water for a non-calcium-based,aqueous wet SO_(x) scrubber. In still another instance, the abovesystems utilize less than about 2% by volume of the waste liquorproduced by a non-calcium-based, aqueous wet SO_(x) scrubber to treatand/or soften raw water for a non-calcium-based, aqueous wet SO_(x)scrubber.

Accordingly, another aspect of the present invention is drawn to asystem for treating and/or softening raw water for a non-calcium-based,aqueous wet SO_(x) scrubber substantially as shown and described herein.

Still another aspect of the present invention is a method for treatingand/or softening raw water for a non-calcium-based, aqueous wet SO_(x)scrubber substantially as shown and described herein.

The various features of novelty which characterize the invention arepointed out with particularity in the claims annexed to and forming apart of this disclosure. For a better understanding of the invention,its operating advantages and specific benefits attained by its uses,reference is made to the accompanying drawings and descriptive matter inwhich exemplary embodiments of the invention are illustrated.

BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is an illustration of a conventional system that is designed totreat raw makeup water for use in a wet flue gas desulfurization (WFGD)system;

FIG. 2 is a plot that illustrates the effect of lime softening on a rawwater whose hardness comes from only calcium and magnesium carbonates(no sulfates were present);

FIG. 3 is a plot illustrating the effect of lime softening on a rawwater whose hardness comes from only calcium and magnesium sulfates (nocarbonates were present);

FIG. 4 is a plot showing the ability of a softening system in accordancewith one embodiment of the present invention to remove calcium from rawwater;

FIG. 5 is a schematic of a raw water softening system in accordance withone embodiment of the present invention where waste liquor from a sodascrubber is used to treat and/or soften raw water; and

FIG. 6 is a schematic of a raw water softening system in accordance withanother embodiment of the present invention where waste liquor from asoda scrubber is used in place of the sulfuric acid in a conventionallime slaking system to treat and/or soften raw water to precipitate theexcess calcium that is generated when the pH is raised high enough toprecipitate magnesium from the system.

DESCRIPTION OF THE INVENTION

The present invention relates generally to the field of emission controlequipment for boilers, heaters, kilns, or other flue gas-, or combustiongas-, generating devices (e.g., those located at power plants,processing plants) and, in particular to a new and useful method andapparatus designed to improve the water supplied to non-calcium-based,aqueous wet SO_(x) scrubbers. In another embodiment, the presentinvention relates to a system and method for softening water for use innon-calcium-based, aqueous wet SO_(x) scrubbers.

Lime softening relies on the relatively low solubility of calciumcarbonate. Solubility expressed in complex ionic systems such as watertreatments systems express the solubility of the various inorganicconstituents by their solubility products. The solubility product ofcalcium carbonate at 25° C. is 2.8×10⁻⁹. The solubility product formagnesium carbonate is a little less at 3.5×10⁻⁸. But, the solubilityproduct for Mg(OH)₂ is 1.3×10⁻¹¹. So, slaked lime, Ca(OH)₂ precipitatescalcium carbonate by converting HCO₃ ⁻ to CO₃ ⁻² and precipitatesmagnesium by increasing the OH⁻ concentration. But, the soda scrubbergenerates sulfite and bisulfite ions in the process of absorbing SO₂from the flue gas. Additionally, calcium sulfite has a solubilityproduct of 6.8×10⁻⁸. This means that in one instance one couldprecipitate calcium from raw water as calcium sulfite directly withoutraising the pH of the raw water at all.

Given this, one embodiment of the present invention involves divertingsome of the waste liquor from a non-calcium-based, aqueous wet SO_(x)scrubber that would be disposed of anyway to a precipitator/crystallizerthat is used to treat and/or soften the raw water feed stream for such awet scrubber. The typical composition of the waste liquor from such ascrubber is: about 70% of the sulfur is in the form of sodium sulfite(Na₂SO₃), while about 30% is in the form of sodium sulfate (Na₂SO₄);about 7 or 8% (depending on pH) is sodium carbonate (Na₂CO₃); and thebalance is impurities. Thus, a small portion of waste liquor can bediverted to the water softener, precipitate the calcium as calciumsulfite and deliver the waste liquor and sludge, so produced, to thewaste pond for disposal. A plot showing the ability of this system toremove calcium, as an example, is presented in FIG. 4.

In this example, if the waste liquor flow to the softener is establishedat a rate of 1% by volume of the raw water flow, the calciumconcentration can be lowered to the same extent as is achievable withthe lime softening system. The softening system overall flow sheet isthus greatly simplified compared to the conventional lime slakingsystem. Thus, one set-up according to the present invention isschematically illustrated in FIG. 5.

As is illustrated in FIG. 5, one system 200 in accordance with thepresent invention includes floc supply line 202, sodium carbonatesolution supply line 203 (optional—if the waste liquor does not haveenough Na₂CO₃), raw water supply line 204 and waste liquor supply line205. The waste liquor that is supplied via waste liquor supply line 205comes from the waste liquor from a non-calcium-based, aqueous wet SO_(x)scrubber. Given this, floc supply line 202, sodium carbonate solutionsupply line 203, raw water supply line 204 and waste liquor supply line205 respectively supply floc, sodium carbonate solution, raw water andwaste liquor to precipitator/crystallizer 212. Precipitator/crystallizer212 also includes at least one agitating device (e.g., a mixer) tofacilitate the mixing of the floc, sodium carbonate solution, raw waterand waste liquor. Once any undesirable solids are permitted to “settleout” and/or precipitate to the bottom of precipitator/crystallizer 212,this treated solution of floc, sodium carbonate solution, raw water andwaste liquor is supplied via supply line 214 to a settler/thickener 216.In settler/thickener 216 the once-treated mixture of floc, sodiumcarbonate solution, raw water and waste liquor is further treated toremove additional unwanted solid particles via the use of one or moreagitating devices (e.g., a mixer). The solids generated by this processare then supplied, with an appropriate amount of solution, to a sludgepond 222, via supply line 218, to permit further settling andreclamation of the solids contained in such a waste solution.Additionally, or in some cases optionally, a portion of the solidsgenerated by settle/thickener 216 are re-supplied, with an appropriateamount of solution, to precipitator/crystallizer 212 via supply line 220to supply seed crystals for the precipitation stage.

Once any undesirable solids are permitted to “settle out” and/orprecipitate to the bottom of settler/thickener 216 the twice-treatedsolution of floc, raw water and waste liquor is supplied via supply line224 to treated water tank 226. From this treated water tank 226, thesuitably treated solution is supplied to a non-calcium-based, aqueouswet SO_(x) scrubber via supply line 234.

In one embodiment, less than about 7% by volume, less than about 5% byvolume, less than about 3% by volume, or even less than about 2% byvolume of the waste soda liquor produced by a non-calcium-based, aqueouswet SO_(x) scrubber is required to treat the raw water going to such anon-calcium-based, aqueous wet SO_(x) scrubber. In another embodiment,the amount of waste soda liquor used and/or recycled into the systemand/or process of the present invention varies depending upon variousfactors, each taken alone or in any combination thereof. Such factorsinclude, but are not limited to, the amount of raw water to be treatedand/or softened, the appropriate pH for the operation of the scrubber,the amount of calcium and/or calcium ions in the raw water feed, and/orthe amount/level of alkalinity in the raw water feed. Given this, thepresent invention is, in some instances, not limited to any cappedamount of waste soda liquor that is used and/or recycled.

In still another embodiment, any amount of waste soda liquor from anon-calcium-based, aqueous wet SO_(x) scrubber can be used in thesystems and/or processes disclosed herein so long as a desiredstoichiometric ratio between the calcium ions in the raw water and thesulfite ions contained in the waste soda liquor is achieved. In oneinstance, a suitable stoichiometric ratio of calcium ions to sulfiteions in the treatment and/or softening process of the present inventionis in the range of about 1:4 to about 4:1, or from about 1:3 to about3:1, or from about 1:2 to about 2:1, or even about 1:1. Here, as well aselsewhere in the specification and claims, individual range limits canbe combined to form additional non-disclosed ranges.

In still another embodiment, the stoichiometric ratios of the presentinvention may be varied to include all increments of one quarter thatfall within the ranges disclosed above. In one instance, a suitablestoichiometric ratio of calcium ions to sulfite ions in the treatmentand/or softening process of the present invention is in the range ofabout 1:3.75 to about 3.75:1, 1:3.50 to about 3.50:1, or even down toabout 1:1.25 to about 1.25:1.

In light of the above, one embodiment of the present inventioneliminates the need to purchase lime and/or sulfuric acid, as well asthe purchase of all of the related equipment needed to store, handle andprocess such compounds. Additionally, the present invention reduces theamount of waste material that must be discarded, i.e. the lime andsulfuric acid that would be consumed in the softening process. Thepresent invention reduces the effluent flow to the waste pond, andprevents any chance that the pond might be shocked with low pH spikescaused by inadvertent sulfuric acid excursions that might otherwisecause SO₂ off-gassing from the pond. Furthermore, the control system ofthe system of the present invention is simplified as well. The limesoftening system of the prior art requires careful control of pHcompared to the waste liquor control that generally requiresproportionate control of the waste liquor flow to the softener inproportion to the raw water flow. Given this, the present invention thusprovides for cost savings in reagent costs, equipment costs, disposalcosts, and control equipment costs.

In another embodiment, illustrated in FIG. 6, waste liquor could be usedin place of the sulfuric acid in a conventional lime slaking system toprecipitate the excess calcium (see FIGS. 2 and 3) that is generatedwhen the pH is raised high enough to precipitate magnesium from thesystem. This method would precipitate the calcium as calcium sulfite butit would not lower the pH. Once the water treatment has reduced thecalcium and magnesium, a high pH treated water can be used in thescrubber to advantage. There is no reason to lower the pH of the treatedwater prior to its use in the scrubber. As illustrated in FIG. 6, system300 includes floc supply line 302, sodium carbonate solution supply line303, raw water supply line 304 and lime supply 306. Lime supply 306supplies lime to detention slaker 308. Detention slaker 308 includestherein at least one agitating device (e.g., a mixer) and is providedwith a water supply line to permit the mixing of the lime from limesupply 306 with water to yield a lime slurry that is supplied, via line310, to precipitator/crystallizer 312. Also supplied toprecipitator/crystallizer 312 are floc via floc supply line 302, sodiumcarbonate solution via sodium carbonate supply line 303 (optional—if thewaste liquor does not have enough Na₂CO₃), and raw water via raw watersupply line 304. Precipitator/crystallizer 312 also includes at leastone agitating device (e.g., a mixer) to facilitate the mixing of thesodium carbonate solution, floc, raw water and lime slurry. Once anyundesirable solids are permitted to “settle out” and/or precipitate tothe bottom of precipitator/crystallizer 312, this treated solution ofsodium carbonate solution, lime, raw water and floc is supplied viasupply line 314 to a settler/thickener 316. In settler/thickener 316 theonce-treated mixture of sodium carbonate solution, lime, raw water andfloc is further treated to remove additional unwanted solid particlesvia the use of one or more agitating devices (e.g., a mixer). The solidsgenerated by this process (predominantly Mg(OH)₂, but may include CaCO₃depending upon the source of the raw water) are then supplied, with anappropriate amount of solution, to a sludge pond 322, via supply line318, to permit further settling and reclamation of the solids containedin such a waste solution. Additionally, or in some cases optionally, aportion of the solids generated by settler/thickener 316 arere-supplied, with an appropriate amount of solution, toprecipitator/crystallizer 312 via supply line 320 to supply seedcrystals for the precipitation stage.

Once any undesirable Mg(OH)₂ solids are permitted to “settle out” and/orprecipitate to the bottom of settler/thickener 316 the twice-treatedsolution of sodium carbonate solution, lime, raw water and floc issupplied via supply line 324 to a second precipitator/crystallizer 327which also includes at least one agitating device (e.g., a mixer) tofacilitate the mixing. In precipitator/crystallizer 327, thethrice-treated mixture of sodium carbonate solution, lime, raw water andfloc is combined with waste liquor from a non-calcium-based, aqueous wetSO_(x) scrubber via waste liquor supply line 328 to precipitate excesscalcium. Once any undesirable solids are permitted to “settle out”and/or precipitate to the bottom of precipitator/crystallizer 327, thistreated solution of sodium carbonate solution, lime, raw water and flocis supplied via supply line 330 to a second settler/thickener 332. Insettler/thickener 332, the thrice-treated mixture of sodium carbonatesolution, lime, raw water and floc is further treated to removeadditional unwanted solid particles via the use of one or more agitatingdevices (e.g., a mixer). The solids generated by this process (CaSO₃)are then supplied, with an appropriate amount of solution, to a sludgepond 340, via supply line 334, to permit further settling andreclamation of the solids contained in such a waste solution.Additionally, or in some cases optionally, a portion of the solidsgenerated by settler/thickener 332 are re-supplied, with an appropriateamount of solution, to precipitator/crystallizer 327 via supply line 336to supply seed crystals for the precipitation stage. The treated wateris then supplied via supply line 338 to a treated water tank 326. Fromthis treated water tank 326, the suitably treated solution is suppliedto a non-calcium-based, aqueous wet SO_(x) scrubber via supply line 342.

Given the above, in one embodiment the present invention relates to asystem designed to treat and/or soften raw water supplied to anon-calcium-based, aqueous wet SO_(x) scrubber, the system comprising:(a) at least one floc supply means; (b) at least one raw water supplymeans; (c) at least one sodium carbonate supply means; (d) at least onewaste liquor supply means, wherein the waste liquor is supplied from aportion of the waste liquor generated by at least one non-calcium-based,aqueous wet SO_(x) scrubber; (e) at least one precipitator/crystallizertank, wherein the at least one floc supply means, the at least one rawwater supply means, the at least one sodium carbonate supply means andthe at least one waste liquor supply means all supply their respectivecompounds to the at least one precipitator/crystallizer tank, andwherein the at least one precipitator/crystallizer tank has at least oneoutlet; and (f) at least one settler/thickener tank that is in fluidcommunication with the at least one outlet of the at least oneprecipitator/crystallizer tank, the at least one settler/thickener tankhaving at least one outlet designed to supply treated water to anon-calcium-based, aqueous wet SO_(x) scrubber.

In another embodiment, the present invention relates to a systemdesigned to treat and/or soften raw water supplied to anon-calcium-based, aqueous wet SO_(x) scrubber, the system comprising:(a) at least one floc supply means; (b) at least one raw water supplymeans; (c) at least one sodium carbonate supply means; (d) at least onelime slurry supply means; (e) at least one firstprecipitator/crystallizer tank, wherein the at least one floc supplymeans, the at least one raw water supply means, the at least one sodiumcarbonate supply means and the at least one lime slurry supply means allsupply their respective compounds to the at least one firstprecipitator/crystallizer tank, and wherein the at least one firstprecipitator/crystallizer tank has at least one outlet; (f) at least onefirst settler/thickener tank that is in fluid communication with the atleast one outlet of the at least one first precipitator/crystallizertank, the at least one first settler/thickener tank having at least oneoutlet; (g) at least one second precipitator/crystallizer tank that isin fluid communication with the at least one outlet of the at least onefirst settler/thickener tank, wherein the at least one secondprecipitator/crystallizer tank has at least one outlet; (h) at least onewaste liquor supply means, wherein the at least one waste liquor supplymeans is in fluid communication with the at least one secondprecipitator/crystallizer tank, wherein the waste liquor is suppliedfrom a portion of the waste liquor generated by at least onenon-calcium-based, aqueous wet SO_(x) scrubber, and wherein the at leastone waste liquor supply means supplies waste liquor to the at least onesecond precipitator/crystallizer tank to precipitate excess calcium; and(i) at least one second settler/thickener tank that is in fluidcommunication with the at least one outlet of the at least one secondprecipitator/crystallizer tank, the at least one secondsettler/thickener tank having at least one outlet designed to supplytreated water to a non-calcium-based, aqueous wet SO_(x) scrubber.

The various supply means of the present invention include, but are notlimited to, tubing, pipes, conduits, hoses, etc. that are designed tocarry, supply and/or contain liquid material.

In one instance, the above systems utilize less than about 7% by volumeof the waste liquor produced by a non-calcium-based, aqueous wet SO_(x)scrubber to treat and/or soften raw water for a non-calcium-based,aqueous wet SO_(x) scrubber. In another instance, the above systemutilize less than about 5% by volume of the waste liquor produced by anon-calcium-based, aqueous wet SO_(x) scrubber to treat and/or softenraw water for a non-calcium-based, aqueous wet SO_(x) scrubber. In stillanother instance, the above systems utilize less than about 3% by volumeof the waste liquor produced by a non-calcium-based, aqueous wet SO_(x)scrubber to treat and/or soften raw water for a non-calcium-based,aqueous wet SO_(x) scrubber. In still another instance, the abovesystems utilize less than about 2% by volume of the waste liquorproduced by a non-calcium-based, aqueous wet SO_(x) scrubber to treatand/or soften raw water for a non-calcium-based, aqueous wet SO_(x)scrubber.

Given the above, the following chemical reactions are provided to offerinsight into the reaction process that occurs in various raw watertreatment and/or softening systems. It should be noted that while thefollowing chemical reactions are provided, that the following chemicalreactions do not necessarily represent all of the reactions taking placeduring the processes discussed herein. Additionally, the presentinvention is not bound to just the chemical reactions shown below.Conventional lime treatment, softening and/or slaking is detailed inreactions (5) and (6), while reaction (7) detail a reaction of interestin the embodiment of FIG. 5, and reactions (8) and (9) detail thereactions of interest in the embodiment of FIG. 6.

FIG. 1—Stage 1—Ca(OH)₂+Ca⁺²+Mg⁺²+CO₃ ⁻²+Na⁺→CaCO₃(s)+Mg(OH)₂(s)+Ca⁺²+OH⁻+Na⁺  (5)

FIG. 1—Stage 2—H₂SO₄+Ca⁺²+2OH⁻+CO₃ ⁻²+Na⁺→CaCO₃(s)+2H₂O+Na⁺+SO₄ ⁻²  (6)

FIG. 5—Ca⁺²+CO₃ ⁻²+2Na⁺+SO₃ ⁻²→CaSO₃(s)+2Na⁺+CO₃ ⁻²  (7)

FIG. 6—Stage 1—Ca(OH)₂+Ca⁺²+Mg⁺²+CO₃ ⁻²+Na⁺→CaCO₃(s)+Mg(OH)₂(s)+Ca⁺²+OH⁻+Na⁺  (8)

FIG. 6—Stage 2—Na₂SO₃+Ca⁺²+2OH⁻→CaSO₃.½H₂O(s)+2Na⁺+2OH⁻  (9)

While specific embodiments of the present invention have been shown anddescribed in detail to illustrate the application and principles of theinvention, it will be understood that it is not intended that thepresent invention be limited thereto and that the invention may beembodied otherwise without departing from such principles. In someembodiments of the invention, certain features of the invention maysometimes be used to advantage without a corresponding use of the otherfeatures. Accordingly, all such changes and embodiments properly fallwithin the scope of the following claims.

What is claimed is:
 1. A system designed to treat and/or soften rawwater supplied to a non-calcium-based, aqueous wet SO_(x) scrubber, thesystem consisting essentially of: (a) at least one floc supply means;(b) at least one raw water supply means, wherein the raw water containsat least calcium ions and magnesium ions; (c) at least one sodiumcarbonate supply means; (d) at least one waste liquor supply means,wherein the waste liquor is supplied from a portion of the waste liquorgenerated by at least one non-calcium-based, aqueous wet SO_(x) scrubberand wherein the waste liquor contains solubilized sulfite ions; (e) atleast one precipitator/crystallizer tank, wherein the at least one flocsupply means, the at least one raw water supply means, the at least onesodium carbonate supply means and the at least one waste liquor supplymeans all supply their respective compounds to the at least oneprecipitator/crystallizer tank, and wherein the at least oneprecipitator/crystallizer tank permits and facilitates a reactionbetween the calcium ions and/or magnesium ions contained in the rawwater, the sodium carbonate and the solubilized sulfite ions containedin the waste liquor supply and wherein the at least oneprecipitator/crystallizer tank has at least one outlet and is designedto remove any undesirable solids from the mixture of compounds suppliedfrom the at least one floc supply means, the at least one raw watersupply means, the at least one sodium carbonate supply means and the atleast one waste liquor supply means so as to generate a treated solutionof floc, sodium carbonate solution, raw water and waste liquor andsupply same to the at least one outlet; and (f) at least onesettler/thickener tank that is in fluid communication with the at leastone outlet of the at least one precipitator/crystallizer tank, the atleast one settler/thickener tank having at least one outlet designed tosupply treated water to a non-calcium-based, aqueous wet SO_(x)scrubber, wherein all of the solubilized sulfite ions necessary for thereaction between the calcium ions and/or magnesium ions contained in theraw water, the sodium carbonate and the solubilized sulfite ions aresupplied from the waste liquor generated by the at least onenon-calcium-based, aqueous wet SO_(x) scrubber, and wherein all of thecalcium ions and/or magnesium ions necessary for the reaction betweenthe calcium ions and/or magnesium ions contained in the raw water, thesodium carbonate and the solubilized sulfite ions are supplied from theraw water.
 2. The system of claim 1, further comprising: (g) at leastone treated water tank that is in fluid communication with the at leastone outlet of the at least one settler/thickener tank, the at least onetreated water tank designed to receive and hold treated water and havingat least one outlet designed to supply treated water to anon-calcium-based, aqueous wet SO_(x) scrubber.
 3. The system of claim1, wherein less than about 7% by volume of the waste liquor produced bythe non-calcium-based, aqueous wet SO_(x) scrubber is supplied to the atleast one waste liquor supply means to treat and/or soften raw water fora non-calcium-based, aqueous wet SO_(x) scrubber.
 4. The system of claim1, wherein less than about 5% by volume of the waste liquor produced bythe non-calcium-based, aqueous wet SO_(x) scrubber is supplied to the atleast one waste liquor supply means to treat and/or soften raw water fora non-calcium-based, aqueous wet SO_(x) scrubber.
 5. The system of claim1, wherein less than about 3% by volume of the waste liquor produced bythe non-calcium-based, aqueous wet SO_(x) scrubber is supplied the atleast one waste liquor supply means to treat and/or soften raw water fora non-calcium-based, aqueous wet SO_(x) scrubber.
 6. The system of claim1, wherein less than about 2% by volume of the waste liquor produced bythe non-calcium-based, aqueous wet SO_(x) scrubber is supply to the atleast one waste liquor supply means to treat and/or soften raw water fora non-calcium-based, aqueous wet SO_(x) scrubber.
 7. The system of claim1, wherein the reaction that takes place in the at least oneprecipitator/crystallizer tank of element (e) is represented by thefollowing chemical reaction: Ca⁺²+CO₃ ⁻²+2Na⁺+SO₃ ⁻²→CaSO₃(s)+2Na⁺+CO₃⁻².
 8. A system designed to treat and/or soften raw water supplied to anon-calcium-based, aqueous wet SO_(x) scrubber, the system comprising:(a) at least one floc supply means; (b) at least one raw water supplymeans, wherein the raw water contains at least calcium ions andmagnesium ions; (c) at least one sodium carbonate supply means; (d) atleast one waste liquor supply means, wherein the waste liquor issupplied from a portion of the waste liquor generated by at least onenon-calcium-based, aqueous wet SO_(x) scrubber and wherein the wasteliquor contains solubilized sulfite ions; (e) at least oneprecipitator/crystallizer tank, wherein the at least one floc supplymeans, the at least one raw water supply means, the at least one sodiumcarbonate supply means and the at least one waste liquor supply meansall supply their respective compounds to the at least oneprecipitator/crystallizer tank, and wherein the at least oneprecipitator/crystallizer tank permits and facilitates a reactionbetween the calcium ions and/or magnesium ions contained in the rawwater, the sodium carbonate and the solubilized sulfite ions containedin the waste liquor supply and wherein the at least oneprecipitator/crystallizer tank has at least one outlet and is designedto remove any undesirable solids from the mixture of compounds suppliedfrom the at least one floc supply means, the at least one raw watersupply means, the at least one sodium carbonate supply means and the atleast one waste liquor supply means so as to generate a treated solutionof floc, sodium carbonate solution, raw water and waste liquor andsupply same to the at least one outlet; and (f) at least onesettler/thickener tank that is in fluid communication with the at leastone outlet of the at least one precipitator/crystallizer tank, the atleast one settler/thickener tank having at least one outlet designed tosupply treated water to a non-calcium-based, aqueous wet SO_(x)scrubber, wherein less than about 7% by volume of the waste liquorproduced by the non-calcium-based, aqueous wet SO_(x) scrubber issupplied to the at least one waste liquor supply means to treat and/orsoften raw water for a non-calcium-based, aqueous wet SO_(x) scrubber.9. The system of claim 8, further comprising: (g) at least one treatedwater tank that is in fluid communication with the at least one outletof the at least one settler/thickener tank, the at least one treatedwater tank designed to receive and hold treated water and having atleast one outlet designed to supply treated water to anon-calcium-based, aqueous wet SO_(x) scrubber.
 10. The system of claim8, wherein less than about 5% by volume of the waste liquor produced bythe non-calcium-based, aqueous wet SO_(x) scrubber is supplied to the atleast one waste liquor supply means to treat and/or soften raw water fora non-calcium-based, aqueous wet SO_(x) scrubber.
 11. The system ofclaim 8, wherein less than about 3% by volume of the waste liquorproduced by the non-calcium-based, aqueous wet SO_(x) scrubber issupplied the at least one waste liquor supply means to treat and/orsoften raw water for a non-calcium-based, aqueous wet SO_(x) scrubber.12. The system of claim 8, wherein less than about 2% by volume of thewaste liquor produced by the non-calcium-based, aqueous wet SO_(x)scrubber is supply to the at least one waste liquor supply means totreat and/or soften raw water for a non-calcium-based, aqueous wetSO_(x) scrubber.
 13. The system of claim 8, wherein the reaction thattakes place in the at least one precipitator/crystallizer tank ofelement (e) is represented by the following chemical reaction: Ca⁺²+CO₃⁻²+2Na⁺+SO₃ ⁻²→CaSO₃(s)+2Na⁺+CO₃ ⁻².